CN102029129B - Axial-radial flow gas-solid phase fixed bed catalytic reactor - Google Patents
Axial-radial flow gas-solid phase fixed bed catalytic reactor Download PDFInfo
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- CN102029129B CN102029129B CN 200910196419 CN200910196419A CN102029129B CN 102029129 B CN102029129 B CN 102029129B CN 200910196419 CN200910196419 CN 200910196419 CN 200910196419 A CN200910196419 A CN 200910196419A CN 102029129 B CN102029129 B CN 102029129B
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Abstract
The invention relates to an axial-radial flow gas-solid phase fixed bed catalytic reactor. The reactor is divided into an upper structure and a lower structure, wherein a catalyst on the upper part has an axial structure, and a catalyst on the lower part has a radial structure; the height of an insulating layer on the upper part of a barrel is 1 to 5 percent of the total height of a catalyst layer; an inlet reaction gas cold shock inlet is formed and an inlet reaction gas cold shock distribution ring pipe is arranged below the insulating layer; the lower part of the barrel is provided with a radial reaction section consisting of heat exchange tubes, a catalyst filled among tube bodies, a reaction gas and product inlet and outlet system and a heat exchange system; the heat exchange tubes are arranged in a regular triangle or concentric circle mode, the length of the heat exchange tubes is 50 to 95 percent of the total height of the catalyst layer, a cooling medium is introduced into the heat exchange tubes, and each tube is provided with four fins; the product inlet and outlet system and the heat exchange system are arranged in the catalyst layer; and a lower supporting plate supports a heat exchange medium distributor. The invention has the advantages that: the temperature of inlet reaction gas can be regulated, the reactor easily exchanges heat, and the production capacity of the reactor is greatly improved on the premise of not increasing the diameter of the reactor.
Description
[technical field]
The present invention relates to the chemical reaction device technical field, relate to a kind of Radial Flow gas solid phase fixed bed catalyst chamber, specifically, relate to a kind of Radial Flow gas solid phase fixed bed catalyst chamber of adjustable mouth reacting gas operating mode.
[background technology]
In the reversible exothermic reactions such as, ammonia synthesis synthetic at methyl alcohol, carbon monodixe conversion, organic compound hydrogenation, dimethyl ether are synthetic, ethylene oxide synthesis, preparing methane by synthetic gas, all use solid particle catalyst, in commercial process on a large scale, all need to use fixed bed catalytic reactor.The characteristics of reversible exothermic reaction are: can discharge a large amount of heats in course of reaction, if heat can not in time be removed, will cause reaction temperature to rise, and the reaction temperature that rises can cause the further increasing of thermal discharge, this can make the very fast temperature runaway of reaction, thereby burns catalyst.Therefore, need to solve the problem of the heat effects reaction result that discharges and the problem that the heat that discharges is reclaimed and utilizes, need in the reversible heat release production process of heavy industrialization, provide scientific and reasonable reactor.
At present, the axial flow gas-solid phase fixed bed catalyst chambers that adopt in suitability for industrialized production more.The continuous expansion of the reversible exothermic reaction industrially scalables such as, ammonia synthesis synthetic along with methyl alcohol, carbon monodixe conversion, organic compound hydrogenation, dimethyl ether are synthetic, ethylene oxide synthesis, preparing methane by synthetic gas, traditional axial flow fixed bed reactors are restricted the space of its volume increase because diameter is subjected to the impact of traffic condition; In addition, its heat transfer effect also can have much room for improvement.
The Radial Flow reactor then large owing to loaded catalyst, flow process is short, the little preferred reactor type that becomes above-mentioned industrial large-sizedization of reversible exothermic reaction equipment of pressure drop.But also there is some shortcoming in traditional radial reactor, and for example: 1. flow process is short, operating mode (temperature, pressure, composition) to reversible exothermic reaction gas requires high, reach or near the optimum response state, still, self but can't regulate traditional radial reactor; Although 2. loaded catalyst is large, the catalytic amount that the Radial Flow reacting gas flows through is also little, if gas purification is bad, more easily causes catalysqt deactivation; 3. the design of radial reactor heat-exchange system arrangement also is a difficult problem.
Chinese patent literature (CN 101249406A) discloses the axial flow reactor that a kind of thermal insulation-cold shock combines with shell of pipe exterior, although having satisfied reversible exothermic reaction, this reactor moves hot requirement, simultaneously can also the by-product middle pressure steam, but, because of the restriction of reactor diameter, its production capacity is subject to certain restrictions.
In addition, Chinese patent literature (CN 101254442A) discloses a kind of pressurized catalysis method for exothermic reaction, it mainly is the centrifugal radial flow reactor that adopts from inside to outside, the shortcoming of this reactor mainly is: 1. reacting gas directly enters reactor, both there be not warm, there is not cooling measure yet, the temperature that enters the reacting gas of reactor mainly relies on the heat exchanger preheating, along with producing the variation of load from 50%～110%, the temperature fluctuation of reacting gas is larger, if the device of regulating temperature is not set in reactor, will causes the reaction operating mode unstable, thereby affect the service life of catalyst; 2. adopt the cross-flow mode because the Radial Flow reactor fluid flows with heat-exchanging tube bundle, this invents described single fin or twin fin not at the higher position of temperature.
[summary of the invention]
The object of the invention is to overcome above-mentioned axially or the shortcoming of Radial Flow reactor, design a kind of diameter of axle of import reacting gas temperature of regulating to fixed bed catalytic reactor, solve the problem of reactor heat exchange difficulty, adapt to the growth requirement that single series maximizes and produces.
Mentality of designing of the present invention is, (reacting gas is axially by upper thermal barrier layer catalyst to design a kind of axial-radial flow reactor, radially by the lower catalytic agent), catalyst mainly is seated in the bottom of reactor, the heat insulation layer that is comprised of catalyst is set on reactor top simultaneously, import reacting gas temperature is risen, guarantee simultaneously to filter out a small amount of poisonous and harmful component that contains in the reacting gas; Distributing barrel import department arranges cold shock gas endless tube outside radial reactor gas, the outer distributing barrel import of gas is stretched in the endless tube bottom, be used for reducing the temperature of import reacting gas, regulate like this making the import reacting gas reach the optimum response operating mode by heat insulation layer and cold shock device, can under the prerequisite that does not increase reactor diameter, increase substantially the production capacity of reactor.
Simultaneously in order to overcome the poor shortcoming of conventional radial flow reactor heat-transfer effect; heat-exchanging tube bundle adopts positive triangle or concentric circles arrangement mode; each heat exchanger tube arranges 4 fins; the fin of each heat exchanger tube points to the central point of positive triangle or concentric circles arrangement; to guarantee that the gaseous phase materials between heat exchanger tube is in turbulence state, the reactor heat exchange efficiency is significantly improved.
For achieving the above object and mentality of designing, the technical scheme that the present invention takes is:
A kind of diameter of axle is to mobile gas solid phase fixed bed catalyst chamber, contain reactor urceolus, upper cover, low head, heat insulation layer, catalyst layer, cylindrical shell is divided into up and down two-part structure, form unified integral body by the reactor urceolus that bears high pressure, be provided with import reacting gas cold shock import, gas feed, manhole and heat transferring medium outlet at upper cover, be provided with at low head and unload the outlet of catalyst mouth, product and heat transferring medium import, it is characterized in that:
Reacting gas is axially by upper thermal barrier layer catalyst, and radially by the lower catalytic agent, cylindrical shell top is 1～5% of catalyst layer total height by the height of the heat insulation layer that catalyst piles;
The import reacting gas cold shock device that is made of the cold shock import of import reacting gas and import reacting gas cold shock distribution endless tube is set under the heat insulation layer, import reacting gas cold shock distribution endless tube wherein stretches into flow manifold, be in height same in the reactor with the heat transferring medium collector, import reacting gas cold shock distribution endless tube is provided with aperture;
The cylindrical shell bottom is conversion zone radially, is made of heat exchanger tube, catalyst, reacting gas and the product turnover system and the heat-exchange system that are seated between body; The device for cleaning pipeline of gas feed is crossed upper cover and is entered in the reactor cylinder, be communicated with (namely with flow manifold through heat insulation layer, reacting gas enters reactor by gas feed, behind the heat insulation layer catalyzer temperature-elevating, after mixing with the cold shock unstripped gas) enter catalyst layer, is communicated with the interflow runner again and exports and be communicated with product on the low head; The device for cleaning pipeline of heat transferring medium import is crossed low head and is entered in the reactor cylinder, be communicated with the heat transferring medium distributor, and be communicated with the heat transferring medium collector by heat exchanger tube, heat transferring medium outlet on pipeline on the heat transferring medium distributor and the upper cover is communicated with, heat exchanger tube is wherein arranged by positive triangle or concentric circles mode, by the card constant spacing, four fins is set on the every heat exchanger tube, logical cooling medium in the heat exchanger tube, loading catalyst between the heat exchanger tube;
Heat transferring medium distributor, heat transferring medium collector are located in the catalyst layer, and the bottom plate of reactor lower part is held the heat transferring medium distributor.
Four fins that arrange on the described heat exchanger tube are set to 90 degrees mutually, and each fin points to the central point of positive triangle or concentric circles arrangement, guarantee the heat transfer effect of Radial Flow reactor.
The length of described heat exchanger tube is 50～95% of catalyst layer total height.
The aperture that described import reacting gas cold shock distribution endless tube is provided with is that 2～3 row's diameters are 1～5 millimeter aperture.
Good effect of the present invention is:
Provide a kind of diameter of axle that can regulate import reacting gas temperature to fixed bed catalytic reactor, solved the problem of reactor heat exchange difficulty, can under the prerequisite that does not increase reactor diameter, increase substantially the production capacity of reactor.
[description of drawings]
Accompanying drawing 1 is the structural representation of a kind of diameter of axle of the present invention to the gas solid phase fixed bed catalyst chamber embodiment 1 that flows;
Accompanying drawing 2 is the structural representation of a kind of diameter of axle of the present invention to the gas solid phase fixed bed catalyst chamber embodiment 2 that flows;
Accompanying drawing 3 is heat exchanger tube arrangement mode and the structural representation that fin is set on it;
Label among the figure is respectively:
1, import reacting gas cold shock import, 2, gas feed, 3, heat insulation layer,
4, import reacting gas cold shock distribution endless tube, 5, the heat transferring medium collector,
6, heat exchanger tube, 7, catalyst layer, 8, the reactor urceolus,
9, bottom plate, 10, unload the catalyst mouth, 11, the product outlet,
12, heat transferring medium import, 13, low head 14, heat transferring medium distributor,
15, interflow runner, 16, card, 17, flow manifold,
18, outer distributing barrel, 19, interior interflow cylinder, 20, upper cover,
21, manhole, 22, heat transferring medium outlet, 23, fin.
[specific embodiment]
Explain further that below in conjunction with accompanying drawing a kind of diameter of axle of the present invention to mobile gas solid phase fixed bed catalyst chamber, provides 4 embodiment.
Embodiment 1
Referring to accompanying drawing 1.A kind of diameter of axle is to mobile gas solid phase fixed bed catalyst chamber, consist of cylindrical shell by the reactor urceolus (8) that bears high pressure, upper cover (20), low head (13), be provided with import reacting gas cold shock import (1), gas feed (2), heat transferring medium outlet (22) and manhole (21) at upper cover (20), be provided with at low head (13) and unload catalyst mouth (10), product outlet (11), heat transferring medium import (12).
Cylindrical shell is divided into up and down two parts, and reacting gas is axially by upper thermal barrier layer catalyst, and radially by the lower catalytic agent, the height of the heat insulation layer that top is piled by catalyst (3) is 1～5% of catalyst layer (7) total height; At the lower import reacting gas cold shock device that is consisted of by import reacting gas cold shock import (1) and import reacting gas cold shock distribution endless tube (4) that arranges of heat insulation layer (3), import reacting gas cold shock distribution endless tube (4) wherein stretches into flow manifold (17), be in height same in the reactor with heat transferring medium collector (5), import reacting gas cold shock distribution endless tube (4) is provided with 1～5 millimeter aperture of 2～3 row's diameters.
The cylindrical shell bottom is conversion zone radially, is made of heat exchanger tube (6), the catalyst that is seated in heat exchanger tube (6), reacting gas and product turnover system and heat-exchange system.The device for cleaning pipeline of gas feed (2) is crossed upper cover (20) and is entered in the reactor cylinder, be communicated with (namely with flow manifold (17) through heat insulation layer (3), reacting gas enters reactor by gas feed, behind the heat insulation layer catalyzer temperature-elevating, after mixing with the cold shock unstripped gas) enter catalyst layer (7), is communicated with interflow runner (15) again and exports (11) and be communicated with product on the low head (13); The device for cleaning pipeline of heat transferring medium import (12) is crossed low head (13) and is entered in the reactor cylinder, be communicated with heat transferring medium distributor (14), and be communicated with heat transferring medium collector (5) by heat exchanger tube (6), heat transferring medium outlet (22) on pipeline on the heat transferring medium collector (5) and the upper cover (20) is communicated with, heat exchanger tube wherein (6) is by card (16) constant spacing, logical cooling medium in the heat exchanger tube (6), loading catalyst between the heat exchanger tube (6), the length of heat exchanger tube (6) are 50～95% of catalyst layer (7) total height.
Heat transferring medium distributor (14), heat transferring medium collector (5) are located in the catalyst layer (7), and the bottom plate of reactor lower part (9) is held heat transferring medium distributor (14).
Because Radial Flow reactor runner is short, in order to guarantee heat transfer effect, heat exchanger tube (6) is arranged (referring to accompanying drawing 3) by positive triangle or concentric circles mode, four fins (23) are set on the every heat exchanger tube (6), fin is mutually 90 ° and sets up, each fin points to the central point of positive triangle or concentric circles arrangement, to guarantee the heat transfer effect of Radial Flow reactor.
Referring to accompanying drawing 2.A kind of diameter of axle is to mobile gas solid phase fixed bed catalyst chamber, and its basic structure is identical with the structure of embodiment 1, and it is different that its main distinction is that gas vent flows to, and concrete difference structure is: product outlet (11) is arranged on the upper cover (20); The device for cleaning pipeline of gas feed (2) is crossed upper cover (20) and is entered in the reactor cylinder, be communicated with flow manifold (17) and enter catalyst layer (7) through heat insulation layer (3), be communicated with interflow runner (15) again, be communicated with by the product outlet (11) on collaborating runner (15) and being arranged on upper cover (20).
Adopt internal diameter of the present invention be 3.6 meters the diameter of axle to mobile gas solid phase fixed bed catalyst chamber, the heat insulation layer (3) of 0.3 meter height is established on cylindrical shell top, the unstripped gas cold shock is set, loading catalyst 85m
3The temperature that is entered reactor by the inlet tower gas of coal based synthetic gas and recycle gaseous components is 189 ℃, and pressure is 8.0MPa, and entering radially after the upon mediation, the temperature of conversion zone (catalyst layer 7) is 215 ℃, hot(test)-spot temperature is 235 ℃ after the section, and the reactor outlet temperature is 232 ℃.Such diameter of axle can be produced 700000 tons of methyl alcohol (calculating by 300 days) per year to mobile gas solid phase fixed bed catalyst chamber, produces 1.2 tons of/ton methyl alcohol of middle pressure steam.
Embodiment 4
Adopt internal diameter of the present invention be 4.0 meters the diameter of axle to mobile gas solid phase fixed bed catalyst chamber, the heat insulation layer (3) of 0.5 meter height is established on cylindrical shell top, the unstripped gas cold shock is set, loading catalyst 120m
3The temperature that is entered reactor by the inlet tower gas of coal based synthetic gas and recycle gaseous components is 210 ℃, and pressure is 8.0MPa, and entering radially after the upon mediation, the temperature of conversion zone (catalyst layer 7) is 215 ℃, hot(test)-spot temperature is 235 ℃ after the section, and the reactor outlet temperature is 232 ℃.Such diameter of axle can be produced 1000000 tons of methyl alcohol (calculating by 300 days) per year to mobile gas solid phase fixed bed catalyst chamber, produces 1.2 tons of/ton methyl alcohol of middle pressure steam.
It more than is preferred embodiment of the present invention; should be pointed out that for those skilled in the art, without departing from the inventive concept of the premise; can also make some improvements and modifications, these improvements and modifications also should be considered within the scope of protection of the present invention.
Claims (3)
1. a diameter of axle is to mobile gas solid phase fixed bed catalyst chamber, contain reactor urceolus (8), upper cover (20), low head (13), heat insulation layer (3), catalyst layer (7), cylindrical shell is divided into up and down two-part structure, form unified integral body by the reactor urceolus (8) that bears high pressure, be provided with import reacting gas cold shock import (1) at upper cover (20), gas feed (2), manhole (21) and heat transferring medium outlet (22), be provided with at low head (13) and unload catalyst mouth (10), product outlet (11) and heat transferring medium import (12) is characterized in that:
Reacting gas is axially by upper thermal barrier layer catalyst, and radially by the lower catalytic agent, the height of the heat insulation layer that cylindrical shell top is piled by catalyst (3) is 1～5% of catalyst layer (7) total height;
The lower import reacting gas cold shock device that is consisted of by import reacting gas cold shock import (1) and import reacting gas cold shock distribution endless tube (4) that arranges of heat insulation layer (3), import reacting gas cold shock distribution endless tube (4) wherein stretches into flow manifold (17), be in height same in the reactor with heat transferring medium collector (5), import reacting gas cold shock distribution endless tube (4) is provided with aperture;
The cylindrical shell bottom is conversion zone radially, is made of heat exchanger tube (6), catalyst, reacting gas and the product turnover system and the heat-exchange system that are seated between body; The device for cleaning pipeline of gas feed (2) is crossed upper cover (20) and is entered in the reactor cylinder, be communicated with flow manifold (17) through heat insulation layer (3) and enter catalyst layer (7), is communicated with interflow runner (15) again and exports (11) and be communicated with product on the low head (13); The device for cleaning pipeline of heat transferring medium import (12) is crossed low head (13) and is entered in the reactor cylinder, be communicated with heat transferring medium distributor (14), and be communicated with heat transferring medium collector (5) by heat exchanger tube (6), heat transferring medium outlet (22) on pipeline on the heat transferring medium distributor (19) and the upper cover (20) is communicated with, heat exchanger tube wherein (6) is arranged by positive triangle or concentric circles mode, by card (16) constant spacing, four fins (23) are set on the every heat exchanger tube (6), logical cooling medium in the heat exchanger tube (6), loading catalyst between the heat exchanger tube (6), the length of described heat exchanger tube (6) are 50～95% of catalyst layer (7) total height;
Heat transferring medium distributor (14), heat transferring medium collector (5) are located in the catalyst layer (7), and the bottom plate of reactor lower part (9) is held heat transferring medium distributor (14).
2. a kind of diameter of axle according to claim 1 is to mobile gas solid phase fixed bed catalyst chamber, it is characterized in that, upper four fins (23) that arrange of described heat exchanger tube (6) are set to 90 degrees mutually, and each fin points to the central point of positive triangle or concentric circles arrangement.
3. a kind of diameter of axle according to claim 1 is characterized in that to mobile gas solid phase fixed bed catalyst chamber, and the aperture that described import reacting gas cold shock distribution endless tube (4) is provided with is that 2～3 row's diameters are 1～5 millimeter aperture.
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| CN 200910196419 CN102029129B (en) | 2009-09-25 | 2009-09-25 | Axial-radial flow gas-solid phase fixed bed catalytic reactor |
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| CN 200910196419 CN102029129B (en) | 2009-09-25 | 2009-09-25 | Axial-radial flow gas-solid phase fixed bed catalytic reactor |
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| CN102029129A CN102029129A (en) | 2011-04-27 |
| CN102029129B true CN102029129B (en) | 2013-01-23 |
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| CN102489222A (en) * | 2011-12-05 | 2012-06-13 | 新地能源工程技术有限公司 | Reaction device for synthesizing methane, and method for synthesizing methane |
| CN102580624B (en) * | 2012-02-21 | 2015-04-15 | 上海国际化建工程咨询公司 | Radial or axial radial fixed bed reactor with support type slot plate distributor |
| CN102580626B (en) * | 2012-03-20 | 2013-10-02 | 南京国昌化工科技有限公司 | Double-shaft radial flow reactor |
| CN102755863A (en) * | 2012-07-20 | 2012-10-31 | 上海国际化建工程咨询公司 | Axial and radial reactor of fixed bed with tube bank wall type internal and external barrels |
| CN103657536B (en) * | 2013-12-10 | 2016-06-01 | 惠生工程（中国）有限公司 | A kind of axial-radial combined type fixed bed catalytic reactor for butylene oxidation-dehydrogenation |
| CN105013408B (en) * | 2015-08-25 | 2017-05-17 | 南京聚拓化工科技有限公司 | Quasi-full-radial fixed bed reactor |
| CN205435687U (en) * | 2015-08-31 | 2016-08-10 | 张淮海 | Radial fixed bed reactor of indirect heat transfer of multistage |
| CN109395669A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of axial-radial flow reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN109395668A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of coupled reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN111732075B (en) * | 2020-06-28 | 2023-06-27 | 南京聚拓化工科技有限公司 | Composite heat-insulating serial temperature-control shift converter device and shift process |
| CN116272295B (en) * | 2023-03-10 | 2024-03-29 | 哈尔滨工程大学 | Ship tail gas treatment device |
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| CN101249406A (en) * | 2008-04-09 | 2008-08-27 | 华东理工大学 | Heat insulation-cold stimulated-shell of pipe exterior cold combined gas solid phase fixed bed catalyst chamber |
| CN101254442A (en) * | 2007-12-07 | 2008-09-03 | 华东理工大学 | Method used for heat liberation pressurization catalytic reaction |
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2009
- 2009-09-25 CN CN 200910196419 patent/CN102029129B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101254442A (en) * | 2007-12-07 | 2008-09-03 | 华东理工大学 | Method used for heat liberation pressurization catalytic reaction |
| CN101249406A (en) * | 2008-04-09 | 2008-08-27 | 华东理工大学 | Heat insulation-cold stimulated-shell of pipe exterior cold combined gas solid phase fixed bed catalyst chamber |
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